CN109996822A - Use the polymerization of chromium-containing catalyst - Google Patents

Use the polymerization of chromium-containing catalyst Download PDF

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Publication number
CN109996822A
CN109996822A CN201780071060.4A CN201780071060A CN109996822A CN 109996822 A CN109996822 A CN 109996822A CN 201780071060 A CN201780071060 A CN 201780071060A CN 109996822 A CN109996822 A CN 109996822A
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method
catalyst
mw
molecular weight
chromium
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CN201780071060.4A
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Chinese (zh)
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林泽榕
E·F·史密斯
K·W·特拉普
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埃克森美孚化学专利公司
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Priority to US62/423,943 priority
Application filed by 埃克森美孚化学专利公司 filed Critical 埃克森美孚化学专利公司
Priority to PCT/US2017/038127 priority patent/WO2018093421A1/en
Publication of CN109996822A publication Critical patent/CN109996822A/en

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    • CCHEMISTRY; METALLURGY
    • C08ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
    • C08FMACROMOLECULAR COMPOUNDS OBTAINED BY REACTIONS ONLY INVOLVING CARBON-TO-CARBON UNSATURATED BONDS
    • C08F210/00Copolymers of unsaturated aliphatic hydrocarbons having only one carbon-to-carbon double bond
    • C08F210/16Copolymers of ethene with alpha-alkenes, e.g. EP rubbers
    • CCHEMISTRY; METALLURGY
    • C08ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
    • C08FMACROMOLECULAR COMPOUNDS OBTAINED BY REACTIONS ONLY INVOLVING CARBON-TO-CARBON UNSATURATED BONDS
    • C08F2/00Processes of polymerisation
    • C08F2/38Polymerisation using regulators, e.g. chain terminating agents, e.g. telomerisation
    • CCHEMISTRY; METALLURGY
    • C08ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
    • C08FMACROMOLECULAR COMPOUNDS OBTAINED BY REACTIONS ONLY INVOLVING CARBON-TO-CARBON UNSATURATED BONDS
    • C08F4/00Polymerisation catalysts
    • C08F4/02Carriers therefor
    • C08F4/025Metal oxides
    • CCHEMISTRY; METALLURGY
    • C08ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
    • C08FMACROMOLECULAR COMPOUNDS OBTAINED BY REACTIONS ONLY INVOLVING CARBON-TO-CARBON UNSATURATED BONDS
    • C08F4/00Polymerisation catalysts
    • C08F4/06Metallic compounds other than hydrides and other than metallo-organic compounds; Boron halide or aluminium halide complexes with organic compounds containing oxygen
    • C08F4/22Metallic compounds other than hydrides and other than metallo-organic compounds; Boron halide or aluminium halide complexes with organic compounds containing oxygen of chromium, molybdenum or tungsten
    • C08F4/24Oxides
    • CCHEMISTRY; METALLURGY
    • C08ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
    • C08FMACROMOLECULAR COMPOUNDS OBTAINED BY REACTIONS ONLY INVOLVING CARBON-TO-CARBON UNSATURATED BONDS
    • C08F4/00Polymerisation catalysts
    • C08F4/42Metals; Metal hydrides; Metallo-organic compounds; Use thereof as catalyst precursors
    • C08F4/44Metals; Metal hydrides; Metallo-organic compounds; Use thereof as catalyst precursors selected from light metals, zinc, cadmium, mercury, copper, silver, gold, boron, gallium, indium, thallium, rare earths or actinides
    • C08F4/52Metals; Metal hydrides; Metallo-organic compounds; Use thereof as catalyst precursors selected from light metals, zinc, cadmium, mercury, copper, silver, gold, boron, gallium, indium, thallium, rare earths or actinides selected from boron, aluminium, gallium, indium, thallium or rare earths
    • CCHEMISTRY; METALLURGY
    • C08ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
    • C08FMACROMOLECULAR COMPOUNDS OBTAINED BY REACTIONS ONLY INVOLVING CARBON-TO-CARBON UNSATURATED BONDS
    • C08F4/00Polymerisation catalysts
    • C08F4/42Metals; Metal hydrides; Metallo-organic compounds; Use thereof as catalyst precursors
    • C08F4/44Metals; Metal hydrides; Metallo-organic compounds; Use thereof as catalyst precursors selected from light metals, zinc, cadmium, mercury, copper, silver, gold, boron, gallium, indium, thallium, rare earths or actinides
    • C08F4/60Metals; Metal hydrides; Metallo-organic compounds; Use thereof as catalyst precursors selected from light metals, zinc, cadmium, mercury, copper, silver, gold, boron, gallium, indium, thallium, rare earths or actinides together with refractory metals, iron group metals, platinum group metals, manganese, rhenium technetium or compounds thereof
    • C08F4/62Refractory metals or compounds thereof
    • C08F4/69Chromium, molybdenum, tungsten or compounds thereof
    • CCHEMISTRY; METALLURGY
    • C08ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
    • C08FMACROMOLECULAR COMPOUNDS OBTAINED BY REACTIONS ONLY INVOLVING CARBON-TO-CARBON UNSATURATED BONDS
    • C08F2500/00Characteristics or properties of obtained polymers; Use thereof
    • C08F2500/04Broad molecular weight distribution
    • CCHEMISTRY; METALLURGY
    • C08ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
    • C08FMACROMOLECULAR COMPOUNDS OBTAINED BY REACTIONS ONLY INVOLVING CARBON-TO-CARBON UNSATURATED BONDS
    • C08F2500/00Characteristics or properties of obtained polymers; Use thereof
    • C08F2500/07High density
    • CCHEMISTRY; METALLURGY
    • C08ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
    • C08FMACROMOLECULAR COMPOUNDS OBTAINED BY REACTIONS ONLY INVOLVING CARBON-TO-CARBON UNSATURATED BONDS
    • C08F2500/00Characteristics or properties of obtained polymers; Use thereof
    • C08F2500/12Melt flow index or melt flow ratio

Abstract

The embodiment of invention disclosed herein is related to adjusting the high load melt index (I of one or more polyolefin polymers during polymerization reaction21.6), the methods of catalyst activities that are one or more or adjusting the polymerization reaction in weight average molecular weight (Mw) and molecular weight distribution (Mw/Mn), which comprises a) make at least one activation chromium-containing catalyst and at least one alkyl aluminum pre-contact to form catalyst mixture in the outside of polymer reactor;B) catalyst mixture is transmitted to the polymer reactor;It contacts the catalyst mixture under the conditions of polymerizable with one or more monomers and forms one or more polyolefin polymers;And d) recycle one or more polyolefin polymers.

Description

Use the polymerization of chromium-containing catalyst

Inventor: Zerong LIN;Edward F.SMITH;Keith W.TRAPP

Related application

This application claims the priority and interests of the sequence number 62/423,943 submitted on November 18th, 2016, the texts The disclosure offered is introduced accordingly by reference.

Technical field

Present invention relates in general to the methods for using chromium-containing catalyst and alkyl aluminum to prepare polyolefin polymer.

Background technique

Polyethylene polymer generally and is widely used as the resin material of various moulding articles and depends on molding side Method and purpose and be required different performance.For example, the polymer with lower molecular weight and Narrow Molecular Weight Distribution is suitable for passing through The product of injection moulding process molding.On the other hand, the polymer with higher molecular weight and wide molecular weight distribution is suitable for by blowing The product of modeling or inflation molding and molding.It in numerous applications, to High molecular weight polyethylene polymer is desirable in.This Quasi-polyethylene polymer has simultaneously for requiring the application (for example, pipe applications) of such intensity to have enough intensity Good processable characteristic.

Polyethylene polymer with wide molecular weight distribution can be by being obtained using the chromium-containing catalyst obtained as follows: The chromium compound being loaded on inorganic oxide carrier is calcined in non-reducing atmosphere to activate it, so that extremely by contained chromium atom Few a part is converted to hexavalent chromium atoms (Cr+6), commonly referred to as philip catalyst.Corresponding material is arranged into titanium dioxide It on silicon, fluidizes and is heated approximately to 400 DEG C -860 DEG C in the presence of oxygen, and chromium is transformed into+6 oxidation state from+3 oxidation state. The second chrome catalysts for high density polyethylene (HDPE) application are by absorbing on dehydrated silica and then with alkyl aluminum for example, second Silylchromate (double-triphenyl silylchromate) composition of oxygroup diethyl aluminum (DEALE) reduction.Referring to example Such as, U.S. Patent number 6,989,344, U.S. Patent Application Publication No. 2003/0232935, WO 2011/161412 and WO 2016/036745。

As in these catalyst each preparation obtained by polyethylene polymer some important aspect of performance not Together.Chromium oxide catalyst on silica is generally acknowledged that the productivity (g PE/g catalyst) having had, also by activity (g PE/g catalyst-hr) measurement, but prepare the polyethylene polymer having lower than desired molecular weight distribution.Based on monosilane The catalyst preparation of base chromate is with desirable molecular weight characteristics (that is, having macromolecule on molecular weight distribution curve Measure acromion wider molecular weight distribution, show two kinds of different molecular weight clusters) polyethylene polymer.

However, the chrome catalysts of activation are for example above-mentioned still may to be met with for those of high density polyethylene (HDPE) (HDPE) preparation By the performance-relevant problem of HDPE with low catalyst activity, fouling, too low or too high MW capacity and/or difference.With the chromium of activation The melt index (MI) and high load melt index of the HDPE of catalyst manufacture generally passes through temperature of reactor control.For some HDPE Grade, temperature of reactor are needed access in fouling temperature to reach target melt index or high load melt index.In addition, being The HDPE product of preparation multiple grades, it is desirable that use multiple catalysts and multiple catalyst activation temperatures.Such requirement makes to make Make method complication.Thus, it is still necessary to the good balance of polymer performance is provided, while being urged using with large-duty activation Agent and/or simplification in terms of manufacturing method are to prepare the HDPE of multi-grade.

Higher molecular weight HDPE can use the chrome catalysts preparation of activation.Lower calcination temperature, for example, 400-700 DEG C is led Cause more low activity.In addition, higher surface area silica promotes higher molecular weight.It is logical before calcification (calcification) It crosses addition aluminium or titanium compound and desired higher molecular weight is reached to the further modification of the chrome catalysts.Therefore, it still needs to It is strong to generate required molecular weight distribution (being indicated by MI or HLMI), good melt to reach the expectation balance of polymer reactor condition Degree and swelling are so that method suitably generates final layered product stiffness and intensity (measuring typically via ESCR).

Summary of the invention

The present invention provides the high load melt index for adjusting one or more polyolefin polymers during polymerization reaction (I21.6), one or more in weight average molecular weight (Mw) and molecular weight distribution (Mw/Mn) or adjust urging for the polymerization reaction The active method of agent, which comprises a) the outside of polymer reactor make at least one activation chromium-containing catalyst with extremely A kind of few alkyl aluminum pre-contact in catalyst slurry mixture;B) catalyst mixture is transmitted to the polymerization reaction Device;It contacts the catalyst mixture under the conditions of polymerizable with one or more monomers and forms one or more polyenes Hydrocarbon polymer;And d) recycle one or more polyolefin polymers.In many embodiments, this method allows to adjust Single active oxidation chrome catalysts are to prepare the chrome catalysts for having and aluminium and/or titanium compound being used to be modified before calcification The HDPE polymer of a certain range MI and HLMI of suitable performance.

Other embodiments of the present invention is described herein, is claimed and becomes bright by following disclosure It is aobvious.

Brief description

Attached drawing is shown can be by (being indicated) that the activation Cr of pre-contact is catalyzed with the DEALE for increasing content by the ratio between Al/Cr High load melt index (the I of the polyethylene of agent preparation21.6) range.

Detailed description of the invention

Before disclosure and description the compounds of this invention, component, composition and/or method, it should be understood that unless another It is described, the present invention is not limited to specific compound, component, composition, reactant, reaction condition, ligand, structure or the like, Because these can change, unless otherwise prescribed.It will also be appreciated that various terms used herein above are merely to description is special Determine embodiment and the intention without being used to limit.

The embodiment of present disclosure provides the height for adjusting one or more polyolefin polymers during polymerization reaction Load meli index (I21.6), one or more in weight average molecular weight (Mw) and molecular weight distribution (Mw/Mn) or described in adjusting The method of the catalyst activity of polymerization reaction, which comprises a) contain at least one activation in the outside of polymer reactor Chrome catalysts and at least one alkyl aluminum in solvent slurry pre-contact to form catalyst mixture;B) catalyst is become silted up Pulp mixture is transmitted to the polymer reactor;C) make the catalyst mixture and one or more monomers in polymerizable condition It is lower contact and form one or more polyolefin polymers;And d) recycle one or more polyolefin polymers.Herein In any embodiment of description, when changing the ratio of alkyl aluminum and chromium-containing catalyst, one or more polyenes High load melt index (the I of hydrocarbon polymer21.6), one or more in weight average molecular weight (Mw) and molecular weight distribution (Mw/Mn) Item or the catalyst activity of the polymerization reaction can change.

Catalyst and catalyst carrier

Chromium, the catalyst containing chromium or based on chromium are well-known and are used for the polymerization of polyolefin polymer.Two kinds extensively The example of the catalyst used includes chromium oxide (CrO3) and silylchromate catalyst, optionally, containing at least one Carrier.Chromium-containing catalyst is much developed in the continuous fluidized bed gas phase and slurry polymerization field for prepare polyethylene polymer Theme.Such catalyst and polymerization are for example, description is in U.S. Patent Application Publication No. 2011/0010938 and beauty State's patent No. 2,825,721,7,915,357,8,129,484,7,202,313,6,833,417,6,841,630,6,989, 344, in 7,504,463,7,563,851,8,420,754 and 8,101,691.

Typically, catalyst system includes supported chrome catalysts and co-catalyst or activator.In general, it is a kind of this The catalyst of sample includes the chromium compound being supported on inorganic oxide matrix.Typical carrier includes the oxygen of silicon, aluminium, zirconium and thorium Compound and their combination.The silica and alumina supporting material of various grades can widely come from many business Source obtains.

In a specific embodiment, carrier is silica.Suitable silica generally has high surface area It is well balanced with big granularity.These silica are typically in the spheric granules form that can be obtained by spray drying process, or In the particle form by polishing, and there is about at least about 300m2The surface area of/g and at least 25 microns of average particle size.It surveys The method of scale area, pore volume and average particle size is disclosed in WO 2011/161412.For higher molecular weight HDPE's Preparation typically uses about 500-600m2The higher surface area of/g, together with modified with Al or Ti.

In several classes of embodiments, silica supports are rigid and have average about 90-110 microns of big granularity With extension until at least 800m2The high surface area of/g.See, for example, WO2011/161412.It is without being bound by theory, high surface area Promote the formation of high molecular weight component, the high molecular weight component is such as HDPE barrels of (HDPE of high load melt index product Drum) and Medium Bulk Containers (intermediate bulk container, IBC) provides improved physical polymeric performance, Especially stress cracking resistance.It also allows modified using the Al or Ti of the low content of Cr/ silica activated catalyst.

Commercially available silica supports include but is not limited to the carrier (880m for being used for PQ PD-11050 catalyst2The surface /g Long-pending and 1.87mL/g pore volume);Carrier (872m for PD-13070 catalyst2/ g surface area and 2.03mL/g pore-body Product), it can be obtained from PQ Corporation, Malvern, Pennsylvania.Before this, PQ silica is limited to about or small In 650m2The surface area of/g, such as their ES 70, CS2133 and CS2050, MS3065 silica.Alternatively, Sylopol 952,955,2408 etc. can from Grace Speciality Catalysts, W.R.Grace&Co., Columbia, Maryland is obtained.

In another embodiment, carrier is silica-titania carrier.Silica-titania carrier is this Field is well known and describes for example, in U.S. Patent number 3,887,494.Silica-titania carrier can also be such as the U.S. Like that by keeping silica and titanium compound " solidifying altogether described in the patent No. 3,887,494,5,096,868 and 6,174,981 Glue " or co-precipitation preparation.

Chromium can by from 0.1,0.5,0.8, the lower limit of 1.0wt% or 1.5wt% to 10wt%, 8wt%, 5wt% or The amount of the upper limit of 3wt% is present in catalyst, and the range of any lower limit to any upper limit is also considered.

Suitable commercially available chromium-containing catalyst includes HA-30, HA30W and HA30LF, and the product of W.R.Grace&Co. contains About 1wt%Cr.Load-type Titanium-chrome catalysts are also commercially available and urge including the modified chromium in the titanium surface derived from PQ Corporation Agent such as C-23307, C-25305, C-25345, C-23305 and C-25307.The modified chrome catalysts allusion quotation in commercially available titanium surface Contain about 1-5wt%Ti and 1wt%Cr to type.Other commercially available catalyst include the catalyst of PD-11050 containing chromium and aluminium table Face is modified PD-13070 chrome catalysts, commercially available from PQ Corporation.

Typically, before the use by suitably being heated in air or in oxygen-enriched atmosphere in non-reducing atmosphere Dry catalyst system is by activation of catalyst.Activation temperature can be 400 DEG C, 450 DEG C, 500 DEG C or 550 DEG C to 900 DEG C, 800 DEG C or 700 DEG C, the range of any lower limit to any upper limit is also considered.In a specific embodiment, activation temperature Degree is about 600 DEG C.Typical heating time can be 30 minutes to 50 hours, wherein 2-20 hours it is usually enough.It is living Change suitably carries out in fluidizing air stream, wherein continuing the fluidizing air stream as material is cooling.

Co-catalyst

Chromium-containing catalyst can be used together at least one co-catalyst or activator.In general, the co-catalysis Agent can be the metal alkyls of the 13rd race's metal.Co-catalyst can be formula MR3Compound, wherein M be the 13rd race gold Belong to (according to the new numbering plan of IUPAC) and each R is independently linear or branching C1Or C2Or C4To C12Or C10Or C8 Alkyl.The mixture of two or more such metal alkyls is also considered, and is included in term as used herein In " co-catalyst ".

In a kind of embodiment, M is aluminium, and co-catalyst is at least one alkyl aluminum.Alkyl aluminum includes triethyl group Aluminium (TEAl), triisobutyl aluminium (TIBAl), tri-n-hexyl aluminum (TNHA), tri-n-octylaluminium (TNOA) and their mixture.

In another kind of embodiment, at least one alkyl aluminum can be alkoxylated alkyl aluminium compound, such as ethoxy Base diethyl aluminum (DEAlE).

In above-mentioned any embodiment, alkyl aluminum and at least one chromium-containing catalyst can be made by 0.01-10.00 Al/Cr molar ratio, by the Al/Cr molar ratio of 0.05-10.00, by the Al/Cr molar ratio of 0.05-8.00, by 0.10-8.00 Al/Cr molar ratio, by the Al/Cr molar ratio of 0.10-5.00, by the Al/Cr molar ratio of 0.50-5.00, or press 1.00-3.00 Al/Cr molar ratio pre-contact.

Polymerization

The embodiment of present disclosure includes polymerization, wherein making monomer (such as ethylene and/or propylene), He Feibi Strategic point, comonomer contact under the conditions of polymerizable with above-mentioned at least one chromium-containing catalyst and at least one co-catalyst.This " polymerizable condition " used in text refers to those conditions, and temperature, pressure including those of skill in the art's selection, reactant are dense Degree, non-essential solvents/diluents, reactant mix/add parameter, and facilitate one kind at least one polymer reactor Or a variety of olefinic monomers are reacted when contacting with activated olefins polymerization catalyst to prepare the condition of required polyolefin polymer.

Here useful monomer includes substituted or unsubstituted C2-C40Alpha-olefin, preferably C2-C20Alpha-olefin, preferably C2-C12 Alpha-olefin, optimal ethylene, propylene, butylene, amylene, hexene, heptene, octene, nonene, decene, endecatylene, dodecylene and it Isomers.In a preferred embodiment, alkene include be ethylene or propylene monomer and it is one or more it is non-must The comonomer wanted, the comonomer include C4-C40Alkene, preferably C4-C20Alkene or preferred C6-C12One of alkene Or it is a variety of.C4-C40Olefinic monomer can be linear, branching or cricoid.C4-C40Cyclic olefin can be strain (strained) Or unstrained (unstrained), monocycle or polycyclic, and may include one or more hetero atoms and/or one or more Functional group.In another preferred embodiment, alkene includes the monomer and non-essential comonomer for being ethylene, described total Polycondensation monomer includes C3-C40Alkene, preferably C4-C20Alkene or preferred C6-C12One of alkene is a variety of.The C3-C40Alkene Monomer can be linear, branching or cricoid.The C3-C40Cyclic olefin can be strain or unstrained, monocycle or polycyclic , and may include hetero atom and/or one or more functional groups.

Illustrative C2-C40Olefinic monomer and non-essential comonomer include ethylene, propylene, butylene, amylene, hexene, Heptene, octene, nonene, decene, endecatylene, dodecylene, norbornene, norbornadiene, dicyclopentadiene, cyclopentene, Cycloheptene, cyclo-octene, cyclo-octadiene, cyclododecene, 7- oxanorbornene, 7- oxanorbornadiene, they replace The isomers of derivative and they, preferably hexene, heptene, octene, nonene, decene, dodecylene, cyclo-octene, 1,5- ring pungent two Alkene, 1- hydroxyl -4- cyclo-octene, 1- acetoxyl group -4- cyclo-octene, 5- methyl cyclopentene, cyclopentene, dicyclopentadiene, norborneol Alkene, norbornadiene and their substitutive derivative, preferably norbornene, norbornadiene and dicyclopentadiene.

Diene monomers include any hydrocarbon structure at least two unsaturated bonds, preferably C4-C30, wherein the unsaturation At least two in key are easy to introduce polymer by stereospecificity or non-cubic specific catalyst (one or more) In.It may further be preferable that diene monomers are selected from α, ω-diene monomers (that is, di-vinyl monomers).In at least one embodiment party In case, diene monomers are linear di-vinyl monomers, for example, containing those of 4-30 carbon atom.The non-limiting example of diene Including butadiene, pentadiene, hexadiene, heptadiene, octadiene, nonadiene, decadinene, 11 carbon diene, 12 carbon diene, ten Three carbon diene, 14 carbon diene, pentadecane diene, 16 carbon diene, 17 carbon diene, 18 carbon diene, 19 carbon diene, two Ten carbon diene, 21 carbon diene, 22 carbon diene, two oleatridecadienes, tetracosadiene, two pentadecane diene, two 16 carbon diene, heptacosadiene, 28 carbon diene, 29 carbon diene, 30 carbon diene, especially preferred diene packet Include 1,6- heptadiene, 1,7- octadiene, 1,8- nonadiene, 1,9- decadinene, 11 carbon diene of 1,10-, 12 carbon two of 1,11- Alkene, 1,12- oleatridecadiene, 14 carbon diene of 1,13- and low molecular weight polybutadiene (Mw is less than 1000g/mol).Ring-type two The non-limiting example of alkene includes cyclopentadiene, vinyl norbornene, norbornadiene, ethylidene norbornene, divinyl Base benzene, dicyclopentadiene or containing more advanced ring in each ring position with and without the diene of substituent group.

The polymerization of present disclosure can be carried out by any suitable mode as known in the art.This can be used Known any suspension, homogeneous, ontology, solution, slurry or gas phase polymerization process in field.These methods can be by interval, half Intermittently or serially mode operation.At least about 90wt% that homogeneous polymerization method is defined as wherein product dissolves in reaction medium Method.The monomer concentration that bulk process is defined as in wherein all raw materials of reactor is 70 volume % or higher method.Or Person, solvent or diluent are not present in or make an addition in reaction medium (the load in addition to being used as catalyst system or other additives The amount that is a small amount of, or usually being coexisted with monomer of body, such as the propane in propylene).

In another embodiment, the method is slurry process.Term as used herein " slurry phase polymerisation process " Refer to the polymerization for wherein making monomer polymerization using loaded catalyst and on the supported catalyst particle.From negative At least 95wt% of the polymer product of supported catalyst in pelletized form, be solid particle (being not dissolved in diluent).

Suitable diluent/solvent for polymerization includes noncoordinating inert fluid.Non-limiting example include straight chain and Branched-chain hydrocarbons such as iso-butane, butane, pentane, isopentane, hexane, isohexane, heptane, octane, 12 carbon alkane and their mixing Object;Cyclic annular and clicyclic hydrocarbon such as hexamethylene, cycloheptane, hexahydrotoluene, methylcycloheptane and their mixture, such as quotient Those (Isopar present on industryTM);For example perfluorinated C of perhalogenation hydrocarbon4-C10Alkane, chlorobenzene and aromatics and alkyl-substituted virtue Compounds of group such as benzene, toluene, mesitylene and dimethylbenzene.Suitable solvent further includes that can serve as monomer or comonomer Liquefied olefines, including but not limited to ethylene, propylene, 1- butylene, 1- hexene, 1- amylene, 3- Methyl-1-pentene, 4- methyl-1-pentene Alkene, 1- octene, 1- decene and its mixture.In a preferred embodiment, aliphatic hydrocarbon solvent is used as solvent, such as isobutyl Alkane, butane, pentane, isopentane, hexane, isohexane, heptane, octane, 12 carbon alkane or their mixture;It is cyclic annular or alicyclic Hydrocarbon, such as hexamethylene, cycloheptane, hexahydrotoluene, methylcycloheptane or their mixture.

Preferred polymerization can be run under any temperature and/or pressure for being suitable for obtaining required polyolefin.Allusion quotation The temperature and/or pressure of type include about 0 DEG C-about 300 DEG C, such as about 20 DEG C-about 200 DEG C, such as about 35 DEG C-big About 150 DEG C, such as about 40 DEG C-about 120 DEG C, such as about 45 DEG C-about 80 DEG C of temperature;About 0.35MPa- is about 10MPa, such as about 0.45MPa- about 6MPa, or the pressure of preferably approximately 0.5MPa- about 4MPa.

Hydrogen can be added to the molecular weight control that polyolefin is used in reactor.In at least one embodiment, Hydrogen presses about 0.001-50psig (0.007-345kPa), such as about 0.01- about 25psig (0.07-172kPa), example As the partial pressure of about 0.1-10psig (0.7-70kPa) is present in polymer reactor.In one embodiment, it adds 600ppm or less hydrogen, or addition 500ppm or less hydrogen or 400ppm or less or 300ppm or less.At it In its embodiment, the addition at least hydrogen of 50ppm or 100ppm or more or 150ppm or more.

In a kind of embodiment, polymerization is gas phase polymerization process.Generally, in the gas for being used to prepare polymer In bed process, make comprising one or more monomers gaseous stream in the presence of a catalyst under reactive conditions continuously Circulate through fluidized bed.The gaseous stream is discharged from the fluidized bed and is recycled back to the reactor.Meanwhile by polymer Product, which is discharged from reactor and adds fresh monomer, substitutes the monomer having polymerize.Typically, gas-phase reactor can be by condensation mould Formula operation, wherein one of above-mentioned diluent/solvent or a variety of inertia condensing agents (ICA) served as in fluidized-bed reactor are used It is hot to improve throughput rate and/or improvement polymer performance in removing.See, e.g., U.S. Patent number 4,543,399;4,588, 790;5,028,670;5,317,036;5,352,749;5,405,922;5,436,304;5,453,471;5,462,999;5, 616,661 and 5,668,228.

In another kind of embodiment, polymerization is slurry phase polymerisation process.Slurry phase polymerisation process generally with 1- about The range or even greater pressure of 50 atmospheric pressure (15psi-735psi, 103kPa-5068kPa) and 0 DEG C-about 120 DEG C Temperature operation.In slurry phase polymerisation process, solid-state, granulated polymer suspension be added to monomer wherein and copolymerization is single Body in the liquid polymerization diluent medium of catalyst together with forming.It will include the suspension of diluent intermittently or continuously from anti- Device is answered to remove, wherein the property of will volatilize component is separated with polymer and recycled (optionally after distillation) to the reactor.With In the liquid diluent usually alkane containing 3-7 carbon atom, preferably branched alkane of polymerisation medium.Used medium exists It should be liquid and relatively inert under polymerizing condition.When a propane medium is used, it should in reaction diluent critical-temperature and pressure Above operation the method.It is preferred that using hexane or isobutane medium.

Chromium-containing catalyst and alkyl aluminum delivering

Above-mentioned polymerization reactor system and polymerization can be using for will be outside reactors in slurry mixture Then pre-contact is used as catalyst mixture to import at least one chromium-containing catalyst and at least one alkyl aluminum of the reactor The transportation system or method of delivering.For example, embodiment provides the method for operation polyolefin reactor, the method includes living Change chromium-containing catalyst in reactor solvent such as iso-butane or slab oil, it is then mixed with the slurry of alkyl aluminum pre-contact It closes object and supplies polymer reactor such as gas-phase reactor or slurry-phase reactor.It can be substantially continuous by the catalyst mixture Ground supplies polymer reactor.Transportation system may include keeping chromium-containing catalyst and the mixer instance that alkyl aluminum uniformly contacts such as static Mixer or stirring container.In addition, every kind of solvent or diluent, such as more high viscosity mineral oil can be required to adjust and be catalyzed containing chromium The contact residence time of agent and the pre-contact of alkyl aluminum.

In several classes of embodiments, pre-contacting steps can be before it will inject polymer reactor and in the outer of reactor Portion carries out online.Delivering can be carried out via a variety of methods.For example, can be by chromium-containing catalyst and alkyl aluminum (or low concentration Alkyl aluminum solutions) have rotation mechanical agitator mixing vessel or online static mixing device in mix, then refer to The downstream line of measured length is to allow the time of contact between chromium-containing catalyst and alkyl aluminum.Alternatively, chromium-containing catalyst and alkyl Pre-contact between aluminium can carry out in replacing pipeline or the container for combining pipeline.In any of these embodiments, contain chromium Time of contact between catalyst and alkyl aluminum can be controlled via to the diluent of feed system addition knots modification, this can For increasing or decreasing time of contact as needed.

The illustrative time of contact of chromium-containing catalyst and alkyl aluminum can be at -150 minutes 1 second, -100 minutes 1 second, 1 - 10 minutes, -90 seconds 1 second, -30 minutes 30 seconds, -120 minutes 2 minutes, -30 minutes 10 minutes or -30 minutes 18 minutes second In range.

Advantageously, embodiments disclosed herein is provided when the ratio of alkyl aluminum and chromium-containing catalyst changes, and is adjusted Or change the high load melt index (I of one or more polyolefin polymers during polymerization reaction21.6), weight average molecular weight (Mw) one or more and in molecular weight distribution (Mw/Mn) or adjust the polymerization reaction catalyst activities have it is flexible The method of property.One of by the following means or a variety of it can adjust the ratio: increase/reduction time of contact;Raising/drop Low diluent concentration;With raising/reduction chromium-containing catalyst and/or the concentration of alkyl aluminum etc..

In several classes of embodiments, the catalyst activity of polymerization reaction is at least 1,500g/g/hr or bigger, at least 1, 750g/g/hr or bigger, at least 2,000g/g/hr or bigger, at least 2,250g/g/hr or bigger, at least 2,500g/g/hr or It is bigger, at least 2,600g/g/hr or bigger, at least 2,750g/g/hr or bigger, at least 3,000g/g/hr or bigger, or at least 3,100g/g/hr or bigger.

Polymer product

Present disclosure further relates to the polyene prepared by the chromium-containing catalyst and co-catalyst and methods described herein The preparation of hydrocarbon polymer.In at least one embodiment, the method includes preparing Alathon or ethylene copolymer, example Such as ethylene-alpha-olefin (preferably C3-C20) copolymer (such as Ethylene/Butylene, ethylene-hexene co-polymers or ethylene-octene copolymerization Object).

In at least one embodiment, the polyolefin polymer prepared here is the homopolymer of ethylene or preferably contains about One or more C of 0-25 moles of %3-C20Olefin comonomer (such as about 0.5-20 moles %, about 1- about 15 rubs Your %, or about 10 moles of % of about 3-) ethylene copolymer.Olefin comonomer can be C3-C12Alpha-olefin, such as third One of alkene, butylene, hexene, octene, decene, dodecylene are a variety of, preferably propylene, butylene, hexene, octene.

Here prepared polyolefin polymer can have about 0.935- about 0.960g/cm3, about 0.940- is big About 0.959g/cm3, about 0.945- about 0.957g/cm3, about 0.945- about 0.955g/cm3, or about 0.945- is big About 0.950g/cm3The density according to ASTM D-4703 and ASTM D-1505/ISO 1183.

Here prepared polyolefin polymer, which can have, is measured by (190 DEG C/2.16kg) of ASTM D-1238-E About 0.01- about 300g/10min, about 0.1- about 100g/10min, about 0.1- about 50g/10min, about 0.1g/10min- about 5.0g/10min, about 0.1g/10min- about 3.0g/10min, about 0.2g/10min- is about 2.0g/10min, about 0.1g/10min- about 1.2g/10min, about 0.2g/10min- about 1.5g/10min, about 0.2g/10min- about 1.1g/10min, about 0.3g/10min- about 1.0g/10min, about 0.4g/10min- is about 1.0g/10min, about 0.5g/10min- about 1.0g/10min, about 0.6g/10min- about 1.0g/10min, about 0.7g/10min- about 1.0g/10min, or about 0.75g/10min- about 0.95g/10min melt index (MI) (MI) or (I2.16)。

Here prepared polyolefin polymer, which can have, is measured by (190 DEG C/21.6kg) of ASTM D-1238-F About 0.1- about 300g/10min, about 0.1- about 100g/10min, about 0.1- about 50g/10min, about 1.0g/ 10min- about 50.0g/10min, about 0.1g/10min- about 35.0g/10min, about 0.1g/10min- is about 30.0g/10min, about 1.0g/10min- about 10.0g/10min, about 1.0g/10min- about 6.0g/10min, about 1.0g/10min- about 5.0g/10min, about 2.0g/10min- about 4.0g/10min, about 0.4g/10min- is about 1.0g/10min, about 0.5g/10min- about 1.0g/10min, about 0.6g/10min- about 1.0g/10min, about 0.7g/10min- about 1.0g/10min, or the high load melt index of about 0.75g/10min- about 0.95g/10min (HLMI) or (I21.6)。

In a kind of embodiment, one or more polyolefin polymers have at least the first high load melt index (I21.6) and at least the second high load melt index (I21.6).At least first high load melt index (I21.6) and it is described extremely Few second high load melt index (I21.6) can be in the range of 0.1-100g/10min or 1-50g/10min.

Here prepared polyolefin polymer can have about 15,000- about 500,000g/mol, about 20, 000- about 250,000g/mol, about 25,000- about 200,000g/mol, about 150,000- about 400,000g/ Mol, about 200,000- about 400,000g/mol, or the weight average molecular weight of about 180,000- about 350,000g/mol (Mw)。

In a kind of embodiment, one or more polyolefin polymers can have at least the first weight average molecular weight (Mw) and at least the second weight average molecular weight (Mw).At least first weight average molecular weight (Mw) and at least second Weight-average molecular Measuring (Mw) can be in the range of 20,000-400,000g/mol or 100,000-350,000g/mol.Mz average molecular weight It will be reported as the index of high MW tail needed for ESCR.

Here prepared polyolefin polymer can have about 1- about 60, and about 5- about 50, about 15- is about 40, or the molecular weight distribution (MWD) or (Mw/Mn) of about 17- about 35.As noted above, the ratio between Mz/Mw is answered This report indicates high MW characteristic.The shape of acromion is also significant.

In a kind of embodiment, one or more polyolefin polymers can have at least the first molecular weight distribution (Mw/Mn) and at least the second molecular weight distribution (Mw/Mn).At least first molecular weight distribution (Mw/Mn) and described at least Two molecular weight distributions (Mw/Mn) can be in the range of 5-50 or 10-40.

Molecular weight distribution (" MWD ") is equivalent to expression formula Mw/Mn.Expression formula Mw/Mn is that weight average molecular weight (Mw) and number are equal The ratio between molecular weight (Mn).Weight average molecular weight provides are as follows:

Number-average molecular weight provides are as follows:

Z- average molecular weight provides are as follows:

The wherein n in previous equationsiIt is with molecular weight MiMolecule number fraction.It is rolled over by using equipped with differential The high-temperature gel permeation chromatography method (Polymer Laboratories) of optical index detector (DRI) measures Mw, Mn and Mw/Mn. Use three Polymer Laboratories PLgel, 10 μm of Mixed-B columns.Rated flow is 1.0mL/min, nominal to infuse Beam product is 300 μ L.Equipped with various feed-lines, column and differential refractometer (DRI detection in the baking oven for being maintained at 160 DEG C Device).Solvent for experiment is the Aldrich examination by the way that the 6 of antioxidant grams of butylated hydroxytoluenes will be used as to be dissolved in 4 liters It is prepared in agent grade 1,2,4- trichloro-benzenes (TCB).Then the TCB mixture is allowed to filter 0.1 μm of Teflon filter.Then TCB is set to deaerate with online degasser before entering in GPC instrument.By the way that dry polymer to be put into vial, add Then mixture is heated about 2 hours at 160 DEG C under continuous shaking to prepare polymer solution by the desired amount of TCB.With weight Analytic approach measures all amounts.Injection concentration is 0.5-2.0mg/ml, and lower concentration is used for the sample of higher molecular weight.It is trying It tests before each sample, purges DRI detector.Then the flow in equipment is increased to 1.0ml/ minutes, and in injection first Stabilize DRI 8 hours.By by generic calibration relationship with a series of monodisperse polystyrenes (PS) standard The column calibration combination that sample carries out is to measure molecular weight.In each elution volume, MW is calculated with following equation:

Wherein the variable with subscript " X " represents test specimen, and represents PS with those of subscript " PS ".In this side In method, aPS=0.67 and KPS=0.000175, and aXAnd KXIt is obtained by disclosed document.Particularly, a/K is for PE=0.695/ 0.000579, for PP=0.705/0.0002288.

The concentration (c) of each point is with following equation by subtracting the DRI signal (I of baseline in chromatogramDRI) calculate:

C=KDRIIDRI/(dn/dc),

Wherein KDRIIt is by the constant of calibration DRI measurement, (dn/dc) is the refractive index increment of system.Particularly, right In both PE and PP, dn/dc=0.109.Quality restores (mass recovery) by the integral area of concentration chromatogram to elution body Long-pending ratio calculates, and plastic injection quality is equal to pre- measurement concentration multiplied by injection loop volume.Unless otherwise mentioned, all molecules Amount is reported with g/mol.

End-use applications

Film, mould can be made by polyolefin polymer prepared by chromium-containing catalyst and co-catalyst and methods described herein Mould product, sheet material, pipe, drum, Medium Bulk Containers (IBC), electric wire and cable coating etc..The film can be by this field Known any conventional method is formed, including extrusion, coextrusion, lamination, blow molding and curtain coating.

The processing method for manufacturing the polyolefin polymer of moulding article is discussed for example, Carraher, Jr., Charles E. (1996): POLYMER CHEMISTRY:AN INTRODUCTION, Marcel Dekker Inc., New York, 512- In 516.Extruded product example includes bucket, medical barrel, electric wire and cable coating, pipe, geomembrane and pond liner.Moulding article Example include list and multi-ply construction, form is bottle, drum, IBC, slot, large-scale hollow product, rigid food containers and toy Deng.

Desirable product includes motor vehicle assembly, sports equipment, and outdoor furniture (such as garden furniture) and sports ground are set It is standby, ship and water transportation component and this other based article.More specifically, the motor vehicle assembly includes such as bumper, lattice Grid, decorative element, mud guard and instrument board, external door and engine cover member, flow spoiler, wind deflector, wheel hub cover, mirror case, Body panel, protectiveness side filler rod, and other inside and outside groups relevant to automobile, truck, ship and other vehicles Part.

Other products further include crate, container, packaging material, labware, office building carpet, instrumentation sample holders and Sampling window;The liquid storage container of medical applications such as bag, capsule and for storing and the bottle of IV infused blood or solution;Pass through spoke The package or container for saving food, other medical equipments, including infusion kits packet, conduit and respiratory therapy are penetrated, and for curing Treat the packaging material of equipment or the food that can be irradiated by γ-or ultraviolet radioactive, including disk and storage liquid especially water, The container of milk or fruit juice, including unit service and in bulk and industrial storage container.

Embodiment

Above-mentioned to retouch it should be understood that although having been combined specific embodiments of the present invention describes the present invention It states and is intended that illustration and is not intended to limit the scope of the invention.Other aspects, advantages and improvements will lead technology belonging to the present invention Technical staff is obvious those of in domain.

Therefore, providing following embodiment is to provide complete disclosure and description for those skilled in the art and be not intended to Limitation inventor regards the range of its invention as.

Catalyst preparation

Catalyst A

In the drying box of nitrogen purging, 0.1g PD-11050 chrome catalysts (1wt%Cr is added into vial; 880m2/ g surface area;With 1.87mL/g pore volume) (can be obtained from PQ Corporation), in drying at 677 DEG C It is activated in air and the dry hexane of 2mL.The 0.04M DEALE solution of 0.5-1.5mL in hexane is added dropwise to containing described In the vortex bottle for activating PD-11050 catalyst, so that the catalyst and the mixing of DEALE solution.By the catalyst and Then DEALE pre-contact 10-30min adds them into reactor for vinyl polymerization.

Catalyst B

PQ PD-11050 chrome catalysts are activated in dry air at 677 DEG C using the same procedure of catalyst A, only It is to prepare catalyst B without using DEALE pre-contact program.

Catalyst C

PQ PD-13070 chrome catalysts are activated in dry air at 677 DEG C using the same procedure for catalyst A (1wt%Cr and 0.6wt%Al;872m2/ g surface area;With 2.03mL/g pore volume) it (can be obtained from PQ Corporation ), only catalyst C is prepared without using DEALE pre-contact program.

Vinyl polymerization

Vinyl polymerization is carried out in 2L Zipper-clave reactor.It is purged at 120-140 DEG C under nitrogen flowing first The reactor 2 hours.Then, 1- hexene and 750mL iso-butane are added in the reactor.The reactor is heated The gross pressure of 410-450psig (2.83-3.10MPa) is pressurized to 99-105 DEG C and with ethylene.Finally by via catalyst Catalyst A, B or C and 0.1g are supported on the TEAL on dehydrated silica by feed pipe addition 250mL iso-butane containing 0.05mmol Scavenger be added reactor.During polymerization, temperature of reactor is controlled via the thermocouple in reactor and external jacket.It presses Feeding ethylene is needed to maintain required gross pressure.It is following to terminate polymerization: to stop reaching close to after 2500g PE/g catalyst productivity It only heats and volatile matter is discharged.

Embodiment 1-7

Ethylene copolymer is carried out with catalyst A.Polymerization and test result are summarized in table 1.

Comparative example 1-6

Ethylene copolymer is carried out with catalyst B and catalyst C.Polymerization and test result are summarized in table 2.

If the data are shown, improving Al/Cr molar ratio leads to higher polyethylene high load melt index (I21.6) and Density.The molecular weight distribution (Mw/Mn) of the embodiment of the present invention is wider, this will improve blow molded product performance, for example, environmental stress resistance Cracking behavior.Embodiment 1-2 and 4-5 with 1-2DEALE/Cr molar ratio also have more real than the comparison with same polymeric condition Apply the higher catalyst activity of example 2.

Attached drawing is shown by the high load capacity melt of the polyethylene with the PD-11050 of DEALE pre-contact activation Cr catalyst preparation Index (I21.6) (embodiment 1-6) be higher than no DEALE pre-contact program PD-11050 activation Cr catalyst preparation poly- second Alkene (comparative example 2).Therefore, the data and attached drawing show to polymerize to have by adjusting the ratio between Al/Cr and Bu Tong gather Physical performance is closed, for example, the various polymer of melt index (MI), high load melt index and/or molecular weight distribution, simultaneously also The catalyst activity maintained.This solution provides the straightforward procedures of the polymer of preparation multiple grades, without always Need the catalyst that swaps out.

Unless otherwise prescribed, phrase "consisting essentially of ..." and " essentially constituting certainly " are not excluded for other steps, element Or the presence (regardless of whether especially referring in the description) of material, on condition that these steps, element or material do not influence this hair Bright basis and novel characteristic, in addition, they are not excluded for usual impurity relevant to element used and material and variant.

For simplicity only specifically disclosing certain numberical ranges herein.However, a certain lower limit can with it is any Other upper limit combinations are for limiting the range for being not known and recording, and similarly, a certain lower limit can be used with any other lower values The range recorded is not known in restriction, equally, a certain upper limit can also be combined with any upper limit is not known record for limiting Range.In addition, each point or single value between two-end-point are also contained in range even if not describing clearly.Therefore, each Point or single value itself can be used as lower limit or the upper limit and combined with other points or single value or other lower limits or the upper limit for limiting not The range being expressly recited.

All existing technical literatures are incorporated herein by quoting, on condition that the disclosure of which not with it is of the invention Description contradicts.In addition, all references recited herein and bibliography (including test procedure, publication, patent, periodical opinion Text etc.) it is incorporated herein by reference of text, on condition that the disclosure of which is not contradicted with description of the invention.

Although according to many embodiments and embodiment, invention has been described, those skilled in the art It can be set after reading present disclosure it will be understood that in the case where not departing from present invention disclosed herein scope and spirit Count other embodiments.

Claims (25)

1. high load melt index (the I of one or more polyolefin polymers during telo merization21.6), weight average molecular weight (Mw) method of the catalyst activities that are one or more or adjusting the polymerization reaction and in molecular weight distribution (Mw/Mn), institute The method of stating includes:
A) make at least one activation chromium-containing catalyst at least one alkyl aluminum pre-contact to be formed in the outside of polymer reactor Catalyst slurry mixture;
B) the catalyst slurry mixture is transmitted to the polymer reactor;
C) catalyst mixture is made to contact and be formed one or more poly- under the conditions of polymerizable with one or more monomers Olefin polymer;With
D) one or more polyolefin polymers are recycled.
2. the method for claim 1 wherein make the alkyl aluminum at least one chromium-containing catalyst by 0.01-10.00's Al/Cr molar ratio pre-contact.
3. the method for claim 1 wherein make the alkyl aluminum at least one chromium-containing catalyst by 0.05-8.00's Al/Cr molar ratio pre-contact.
4. the method for claim 1 wherein make the alkyl aluminum at least one chromium-containing catalyst by 0.10-5.00's Al/Cr molar ratio pre-contact.
5. the method for claim 1 wherein make the alkyl aluminum at least one chromium-containing catalyst by 1.00-3.00's Al/Cr molar ratio pre-contact.
6. the method for any one of the claims, wherein when changing the ratio of alkyl aluminum and chromium-containing catalyst, institute State the high load melt index (I of one or more polyolefin polymers21.6), weight average molecular weight (Mw) and molecular weight distribution (Mw/ Mn the catalyst activity of one or more or described polymerization reactions in) changes.
7. method for claim 6, wherein there is one or more polyolefin polymers at least the first high load capacity melt to refer to Number (I21.6) and at least the second high load melt index (I21.6)。
8. method for claim 7, wherein at least first high load melt index (I21.6) and at least second high load capacity Melt index (MI) (I21.6) in the range of 0.1-100g/10min.
9. method for claim 7, wherein at least first high load melt index (I21.6) and at least second high load capacity Melt index (MI) (I21.6) in the range of 1-50g/10min.
10. the method for any one of the claims, wherein one or more polyolefin polymers have at least first Weight average molecular weight (Mw) and at least the second weight average molecular weight (Mw).
11. method for claim 10, wherein at least first weight average molecular weight (Mw) and at least second Weight-average molecular (Mw) is measured in the range of 20,000-400,000g/mol.
12. method for claim 10, wherein at least first weight average molecular weight (Mw) and at least second Weight-average molecular (Mw) is measured in the range of 100,000-350,000g/mol.
13. the method for any one of the claims, wherein one or more polyolefin polymers have at least first Molecular weight distribution (Mw/Mn) and at least the second molecular weight distribution (Mw/Mn).
14. the method for claim 13, wherein at least first molecular weight distribution (Mw/Mn) and at least second molecular weight (Mw/Mn) is distributed in the range of 5-50.
15. the method for claim 13, wherein at least first molecular weight distribution (Mw/Mn) and at least second molecular weight (Mw/Mn) is distributed in the range of 10-40.
16. the method for any one of the claims, wherein the pre-contact was carried out with -100 minutes 1 second periods.
17. the method for any one of the claims, wherein the pre-contact was carried out with -30 minutes 30 seconds periods.
18. the method for any one of the claims, wherein at least one chromium-containing catalyst includes chromium oxide (CrO3) And/or silylchromate catalyst, optionally contain carrier.
19. the method for claim 18, wherein the carrier includes silica, aluminium oxide, zirconium oxide, thorium oxide or theirs is mixed Close object.
20. the method for any one of the claims, wherein at least one alkyl aluminum is that alkoxylated alkyl calorize is closed Object.
21. the method for claim 20, wherein the alkoxylated alkyl aluminium compound is diethylaluminum ethoxide.
22. the method for any one of claim 1-19, wherein at least one alkyl aluminum is selected from triethyl aluminum, triisobutyl Aluminium, tri-n-hexyl aluminum, tri-n-octylaluminium and their mixture.
23. the method for any one of the claims, wherein the catalyst activity is at least 2,000g/g/hr or bigger.
24. the method for any one of the claims, wherein the catalyst activity is at least 2,250g/g/hr or bigger.
25. the method for any one of the claims, wherein the catalyst activity is at least 2,500g/g/hr or bigger.
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Family Cites Families (29)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
LU34020A1 (en) 1953-01-27 1956-02-06
US3158594A (en) * 1959-11-20 1964-11-24 Grace W R & Co Polymer process and catalyst
US3887494A (en) 1970-11-12 1975-06-03 Phillips Petroleum Co Olefin polymerization catalyst
US4543399A (en) 1982-03-24 1985-09-24 Union Carbide Corporation Fluidized bed reaction systems
US4588790A (en) 1982-03-24 1986-05-13 Union Carbide Corporation Method for fluidized bed polymerization
US5096868A (en) 1987-10-21 1992-03-17 Mobil Oil Corporation Catalyst composition for polymerizing alpha-olefins and alpha-olefins polymerization therewith
FR2634212B1 (en) 1988-07-15 1991-04-19 Bp Chimie Sa Apparatus and process for polymerizing olefins in gas phase in a fluidized bed reactor
US5436304A (en) 1992-03-19 1995-07-25 Exxon Chemical Patents Inc. Process for polymerizing monomers in fluidized beds
US5462999A (en) 1993-04-26 1995-10-31 Exxon Chemical Patents Inc. Process for polymerizing monomers in fluidized beds
US5352749A (en) 1992-03-19 1994-10-04 Exxon Chemical Patents, Inc. Process for polymerizing monomers in fluidized beds
US5317036A (en) 1992-10-16 1994-05-31 Union Carbide Chemicals & Plastics Technology Corporation Gas phase polymerization reactions utilizing soluble unsupported catalysts
EP0699212A1 (en) 1993-04-26 1996-03-06 Exxon Chemical Patents Inc. Process for polymerizing monomers in fluidized beds
ZA9403399B (en) 1993-05-20 1995-11-17 Bp Chem Int Ltd Polymerisation process
US5453471B1 (en) 1994-08-02 1999-02-09 Carbide Chemicals & Plastics T Gas phase polymerization process
US5616661A (en) 1995-03-31 1997-04-01 Union Carbide Chemicals & Plastics Technology Corporation Process for controlling particle growth during production of sticky polymers
US6174981B1 (en) 1998-12-17 2001-01-16 Phillips Petroleum Company Polymerization process
CN1616497A (en) * 2000-07-05 2005-05-18 巴塞尔聚烯烃有限公司 Suspended chrome catalyst containing titanium and the use thereof for producing ethylene homopolymers and copolymers
AU2003245406A1 (en) 2002-06-17 2003-12-31 Exxonmobil Chenical Patents Inc. Polymerization process
US6989344B2 (en) 2002-12-27 2006-01-24 Univation Technologies, Llc Supported chromium oxide catalyst for the production of broad molecular weight polyethylene
US6833417B2 (en) 2002-12-31 2004-12-21 Univation Technologies, Llc Processes for transitioning between chrome-based and mixed polymerization catalysts
US6841630B2 (en) 2002-12-31 2005-01-11 Univation Technologies, Llc Processes for transitioning between chrome-based and mixed polymerization catalysts
CN100451039C (en) 2003-03-28 2009-01-14 联合碳化化学及塑料技术有限责任公司 Chromium-based catalysts in mineral oil for production of polyethylene
US8129484B2 (en) 2005-07-27 2012-03-06 Univation Technologies, Llc Blow molding polyethylene resins
US20070027276A1 (en) 2005-07-27 2007-02-01 Cann Kevin J Blow molding polyethylene resins
EP2247630B1 (en) 2008-02-27 2016-02-24 Univation Technologies, LLC Modified chromium-based catalysts and polymerization processes for using the same
BRPI0923478A2 (en) 2008-12-22 2018-12-26 Univation Tech Llc systems and processes for polymer manufacturing
CN102448999B (en) * 2009-06-26 2015-01-21 日本聚乙烯株式会社 Polyethylene resin, catalyst used for production of the same, method for producing the same, hollow plastic molded article containing polyethylene resin, and use of the hollow plastic molded article
HUE030161T2 (en) 2010-06-24 2017-04-28 Pq Corp Catalyst supports, catalysts and their manufacture and use
SG10201801623QA (en) 2014-09-02 2018-04-27 Univation Tech Llc Polyolefin production with chromium-based catalysts

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